CN1070926C - Apparatus for manufacturing molten pig iron and reduced iron by utilizing fluidized bed, and method therefor - Google Patents
Apparatus for manufacturing molten pig iron and reduced iron by utilizing fluidized bed, and method therefor Download PDFInfo
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- CN1070926C CN1070926C CN98802717A CN98802717A CN1070926C CN 1070926 C CN1070926 C CN 1070926C CN 98802717 A CN98802717 A CN 98802717A CN 98802717 A CN98802717 A CN 98802717A CN 1070926 C CN1070926 C CN 1070926C
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- reduction furnace
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- bed reduction
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 372
- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000004519 manufacturing process Methods 0.000 title claims description 5
- 229910000805 Pig iron Inorganic materials 0.000 title description 5
- 229910052742 iron Inorganic materials 0.000 claims abstract description 153
- 238000002844 melting Methods 0.000 claims abstract description 78
- 230000008018 melting Effects 0.000 claims abstract description 78
- 239000003245 coal Substances 0.000 claims abstract description 30
- 235000019738 Limestone Nutrition 0.000 claims abstract description 15
- 239000006028 limestone Substances 0.000 claims abstract description 14
- 239000000446 fuel Substances 0.000 claims abstract description 13
- 238000002309 gasification Methods 0.000 claims abstract description 5
- 239000007789 gas Substances 0.000 claims description 150
- 239000000428 dust Substances 0.000 claims description 91
- 239000000654 additive Substances 0.000 claims description 73
- 230000000996 additive effect Effects 0.000 claims description 72
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 50
- 238000001354 calcination Methods 0.000 claims description 48
- 238000002360 preparation method Methods 0.000 claims description 29
- 239000002912 waste gas Substances 0.000 claims description 28
- 235000012255 calcium oxide Nutrition 0.000 claims description 26
- 239000000292 calcium oxide Substances 0.000 claims description 26
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 17
- 239000001301 oxygen Substances 0.000 claims description 17
- 229910052760 oxygen Inorganic materials 0.000 claims description 17
- 239000012530 fluid Substances 0.000 claims description 14
- 239000002994 raw material Substances 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 8
- 238000003723 Smelting Methods 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 5
- 238000002485 combustion reaction Methods 0.000 claims description 4
- 238000002347 injection Methods 0.000 claims description 4
- 239000007924 injection Substances 0.000 claims description 4
- 230000003750 conditioning effect Effects 0.000 claims 1
- 238000006722 reduction reaction Methods 0.000 description 139
- 238000010586 diagram Methods 0.000 description 7
- 230000002829 reductive effect Effects 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 230000001105 regulatory effect Effects 0.000 description 5
- 239000002802 bituminous coal Substances 0.000 description 4
- SZVJSHCCFOBDDC-UHFFFAOYSA-N iron(II,III) oxide Inorganic materials O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000002893 slag Substances 0.000 description 4
- 238000011144 upstream manufacturing Methods 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 239000000571 coke Substances 0.000 description 2
- 235000009508 confectionery Nutrition 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- 239000007858 starting material Substances 0.000 description 2
- 239000004575 stone Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000004939 coking Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000155 melt Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0006—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state
- C21B13/0013—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state introduction of iron oxide into a bath of molten iron containing a carbon reductant
- C21B13/002—Reduction of iron ores by passing through a heated column of carbon
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
- C21B2100/44—Removing particles, e.g. by scrubbing, dedusting
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/60—Process control or energy utilisation in the manufacture of iron or steel
- C21B2100/64—Controlling the physical properties of the gas, e.g. pressure or temperature
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture Of Iron (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
公开一种使用细铁矿石制备铁水的装置和方法。使用煤产生还原性气体，并以简单而有效的方式使用细铁矿石制得铁水和还原铁。直接使用煤作为燃料制备铁水。将高温还原性气体从熔化气化炉送到流化床石灰石煅烧炉以煅烧石灰石；还原性气体被供入第二流化床还原炉以便直接制备还原铁；从第二流化床还原炉排出的气体被供入第一流化床还原炉(位于第二流化床还原炉上方)，以便预热和预还原细铁矿石；以及煅烧后的石灰石和最后还原铁被供入熔化气化炉以制备铁水。
A device and method for preparing molten iron using fine iron ore are disclosed. Coal is used to generate reducing gas and fine iron ore is used to produce molten iron and reduced iron in a simple and efficient manner. Directly use coal as fuel to prepare molten iron. High-temperature reducing gas is sent from the melting and gasifier to the fluidized bed limestone calciner to calcine limestone; the reducing gas is fed into the second fluidized bed reduction furnace to directly produce reduced iron; it is discharged from the second fluidized bed reduction furnace The gas is fed into the first fluidized bed reduction furnace (located above the second fluidized bed reduction furnace) in order to preheat and pre-reduce fine iron ore; and the calcined limestone and finally reduced iron are fed into the melting gasification Furnace to prepare molten iron.
Description
Invention field
The present invention relates to utilize fine iron ore to prepare the device of liquid pig iron and direct-reduced iron, and utilize this device to prepare the method for liquid pig iron.
Background of invention
United States Patent (USP) 4,978,387 disclose a kind of former iron ore and coal of typically utilizing in the method for not carrying out preparing under the pretreated situation liquid pig iron.
According to this United States Patent (USP), directly use former iron ore and coal, so that can skip the pre-treatment step such as sintering and coking, thereby simplify production stage and manufacturing facility.
As shown in Figure 1, United States Patent (USP) 4,978,387 device 400 comprises: melting gasifier 410 is used for gasification of coal and smelting reduction iron; Filling bed type pre-reducing furnace 432 is used to the reducing gas indirect reduction iron ore that utilizes melting gasifier 410 to produce; And other utility appliance.
Described utility appliance comprises: cyclone separator 411; Recirculation unit 412; Fusing calcining furnace 413; And Venturi scrubber 433 and 434.
In melting gasifier 410, coal is gasified to produce the reducing gas of indirect reduction iron ore.And, the heat melts that utilize to produce in pre-reducing furnace 432 by the reduced iron of indirect reduction.Simultaneously, pre-reducing furnace 432 utilizes the former iron ore of reducing gas indirect reduction and the additive of melting gasifier 410.The reduced iron that makes like this is continuously discharged in the melting gasifier 410.
Yet in the method, the form that starting material can agglomerate (8-35mm) is used, and is therefore restricted to starting material.That is 80% of the iron ore product is fine iron ore in the world, and aforesaid device only can use agglomerate iron ore and expensive particle, therefore causes major defect.
Simultaneously, United States Patent (USP) 5,192,486 disclose the direct-reduced iron ore device that uses fine iron ore.
As shown in Figure 2, this device 500 comprises: fluidized bed type preheats stove 544, is used for by means of 547 heated hot air heated preheating iron ores in the combustion chamber; 3 grades of reduction furnaces 541,542,543; Gas reforming stove 545 is used to produce reducing gas; Heat exchanger 546 is used for heated air converter 545; Gas sweetening washer 549,550; And briquetting machine 516.
The gas reforming stove transforms Sweet natural gas, is used for the reducing gas of reducing iron ore with generation.Heat exchanger 546 thermal conversion gas are supplied with final reduction furnace 541 subsequently.Reducing gas is purified by gas sweetening washer 549, so that circulate by heat exchanger 546 continuously by second pre-reducing furnace 542 and first pre-reducing furnace 543.Fine iron ore is fed preheating oven so that be preheated, and passes through first pre-reducing furnace, 543, the second pre-reducing furnaces 542 and final reduction furnace 541 subsequently so that finally reduced.Reduced iron is agglomerated into agglomerate by briquetting machine 516.
Aforesaid device uses Sweet natural gas, requires 4 grades of fluidized bed type stoves.Therefore, equipment is very complicated, correspondingly, original device cost height, operation is got up also very complicated.
Summary of the invention
The present invention is intended to overcome the shortcoming of above-mentioned prior art.
Therefore, the purpose of this invention is to provide a kind of apparatus and method of using fine iron ore to prepare molten iron, wherein, use coal to produce reducing gas, and with simple and efficient manner uses fine iron ore to make molten iron and reduced iron.
For part and whole above-mentioned purpose that realizes, the equipment characteristic of the preparation molten iron that direct use coal according to the present invention acts as a fuel is: high-temperature reductibility gas is delivered to fluidized-bed limestone calcination stove with calcined limestone from melting gasifier; Reducing gas is infeeded second fluidized bed reduction furnace so that directly prepare reduced iron; Infeeded first fluidized bed reduction furnace (being positioned at second fluidized bed reduction furnace top) from the second fluidized bed reduction furnace expellant gas, so that preheating and prereduction fine iron ore; And the Wingdale after the calcining is infeeded melting gasifier with the preparation molten iron with last reduced iron.
According to another aspect of the present invention, the apparatus features of the preparation molten iron that direct use coal according to the present invention acts as a fuel is: high-temperature reductibility gas is delivered to fluidized-bed limestone calcination stove with calcined limestone from melting gasifier; Reducing gas is infeeded second fluidized bed reduction furnace so that directly prepare reduced iron; Infeeded first fluidized bed reduction furnace (being positioned at second fluidized bed reduction furnace top) from the second fluidized bed reduction furnace expellant gas, so that preheating and prereduction fine iron ore, thereby the preparation reduced iron.
According to another aspect of the present invention, the apparatus features of the preparation molten iron that direct use coal according to the present invention acts as a fuel is: the high-temperature reductibility gas in the melting gasifier is delivered to the 3rd fluidized bed reduction furnace with final reduction and calcining fine iron ore and thin additive; This reducing gas is infeeded second fluidized bed reduction furnace so that prereduction for the second time and calcining fine iron ore and thin additive; Infeeded first fluidized bed reduction furnace (being positioned at second fluidized bed reduction furnace top) from the second fluidized bed reduction furnace expellant gas, so that prereduction for the first time and calcining fine iron ore and thin additive, thereby the preparation molten iron.
According to another aspect of the present invention, provide the method for utilizing said apparatus to prepare molten iron.
Description of drawings
Above-mentioned purpose of the present invention and other advantages will become apparent by describing the preferred embodiments of the present invention in detail with reference to accompanying drawing.
Fig. 1 is the synoptic diagram of existing molten iron preparation facilities;
Fig. 2 is the synoptic diagram of existing another molten iron preparation facilities;
Fig. 3 is the synoptic diagram of molten iron preparation facilities of the present invention;
Fig. 4 is the synoptic diagram of reduced iron preparation facilities of the present invention;
Fig. 5 is another embodiment of molten iron preparation facilities of the present invention.
Preferred embodiment
Fig. 3 is the synoptic diagram of molten iron preparation facilities of the present invention.As shown in Figure 3, molten iron preparation facilities 100 of the present invention comprises: melting gasifier 11 is used for the iron ore behind gasification of coal and the smelting reduction; The 3rd fluidized bed calcination stove 12 is used to utilize melting gasifier 11 expellant gas calcined limestones; Second fluidized bed reduction furnace 13 is used for the indirect reduction fine iron ore; First fluidized bed reduction furnace 14 is used for preheating and prereduction fine iron ore; Dust cyclone separator 111 is used for (isolated from the reducing gas of melting gasifier 11) dust is sent into dust recirculation unit 112, and (isolated from dust) waste gas is supplied with the 3rd fluidized bed calcination stove 12; Be installed in the fusing burner 113 on the melting gasifier 11, be used for the fine iron ore from dust recirculation unit 112 is ejected into melting gasifier 11, and circulation cyclone separator 121,131,141, be used for catching the fine dust that first to the 3rd fluid bed furnace 12,13,14 is discharged gas, and dust is recycled to each fluid bed furnace.
Device according to the present invention preferably includes: Venturi scrubber 15 is used to accept the first circulation cyclone separator, 141 expellant gas of first class pool furnace 14, to catch and to cool off remaining dust; And/or be positioned at second and first gas heater 132 and 142 of second fluid bed furnace 13 and first class pool furnace 14 upstreams, be used to accept oxygen and heat reducing gas.
Raw material supply pipe 14f is connected with first fluidized bed reduction furnace 14, is used to supply fine iron ore and additive.First fluidized bed reduction furnace 14 links to each other with second fluidized bed reduction furnace 13 by the first reduced iron delivery pipe 14a, with the supply iron ore.And stove 14 links to each other with second fluid bed furnace 13 by the first feed tube 14b, with supply gas.The first exhaust pipe 14c links to each other with the top of stove 14, and with discharging waste gas, pipe 14c links to each other with the first circulation cyclone separator 141.
And first fluidized bed reduction furnace 14 is connected to first cyclone separator 141 to accept dust by the first dust circulation tube 14d.
Venturi scrubber 15 is connected on the first circulation cyclone separator 141 by exhaust pipe 14e.
Second fluidized bed reduction furnace 13 is communicated with melting gasifier 11 by the second reduced iron delivery pipe 13a.Stove 13 bottoms are communicated with the 3rd fluidized bed calcination stove 12 by the second feed tube 13b, to accept gas.The 3rd waste gas delivery pipe 13c links to each other with discharging waste gas with the top of stove 13.This exhaust pipe 13c is communicated with the second circulation cyclone separator 131.
The 4th exhaust pipe 13e links to each other with the second circulation cyclone separator 131 by the first feed tube 14b, is used for giving first fluidized bed reduction furnace 14 with waste gas feed, and waste gas and dust separation are opened simultaneously.First gas heater 142 is installed between the first feed tube 14b and the 4th exhaust pipe 13e.
And second fluidized bed reduction furnace 13 links to each other with the second circulation cyclone separator 131 by dust circulation tube 13d, to accept the dust from it.
The 3rd fluidized bed calcination stove 12 links to each other with Wingdale supply pipe 12f, and the latter links to each other with Wingdale source (not shown) again, so that the supply Wingdale.And stove 12 links to each other with unslaked lime delivery pipe 12a, is used to discharge the unslaked lime after the calcining.Pipe 12a links to each other with the second reduced iron delivery pipe 13a.Therefore, the 3rd fluidized bed calcination stove 12 is communicated with melting gasifier 11 by the unslaked lime delivery pipe 12a and the second reduced iron delivery pipe 13a.
The 3rd fluidized bed calcination stove 12 bottoms link to each other to accept gas with dust cyclone separator 111 by the 3rd feed tube 12b.And the 5th exhaust pipe 12c links to each other with the top of stove 12, and with emission gases, the 5th exhaust pipe 12c links to each other with the 3rd circulation cyclone separator 121.
The 3rd circulation cyclone separator 121 links to each other with the 6th exhaust pipe 12e, and the latter links to each other with feed tube 13b again, is used for waste gas feed to second fluidized bed reduction furnace 13, and this moment, dust was separated from the gas.Second gas heater 132 is preferably mounted between the second feed tube 13b and the 6th exhaust pipe 12e.
Calcining furnace 12 links to each other with the 3rd circulation cyclone separator 121 by the 3rd dust circulation tube 12d, to accept dust.
Reducing gas delivery pipe 11a links to each other with melting gasifier 11, and it also links to each other with dust cyclone separator 111 simultaneously.Therefore, melting gasifier 11 is communicated with supply gas with dust cyclone separator 111.
Fig. 4 is the synoptic diagram of reduced iron preparation facilities of the present invention.As shown in Figure 4, different with the smelting reduction device 100 among Fig. 3, reduced iron preparation facilities 200 structures make: the second reduced iron delivery pipe 13a of second fluidized bed reduction furnace 13 does not link to each other with melting gasifier 11, is in communication with the outside or is communicated with briquetting machine 16 but make.
And different with the smelting reduction device 100 among Fig. 3 is that reduced iron preparation facilities 200 of the present invention makes: the second reduced iron delivery pipe 13a of second fluidized bed reduction furnace 13 does not link to each other with melting gasifier 11, is communicated with but make with the external world or briquetting machine 16.Simultaneously, unslaked lime supply pipe 12g is connected between fluidized bed calcination stove 12 and the briquetting machine 16, and being used in the future, the unslaked lime of self-fluidized type bed calcinator 12 is fed to briquetting machine 16.
Fig. 5 is the synoptic diagram of the another embodiment of molten iron preparation facilities of the present invention.As shown in Figure 5, molten iron preparation facilities 300 comprises: melting gasifier 31 is used for the iron ore behind gasification of coal and the smelting reduction; The 3rd fluidized bed reduction furnace 32 is used to utilize final reducing fine iron ore of melting gasifier 31 expellant gas and the thin additive of calcining; Second fluidized bed reduction furnace 33 is used for fine iron ore of prereduction for the second time and the thin additive of calcining; First fluidized bed reduction furnace 34 is used for fine iron ore of prereduction for the first time and thin additive; Dust cyclone separator 311 is used for (isolated from reducing gas) dust is sent into dust recirculation unit 312, and (isolated from dust) waste gas is supplied with the 3rd fluidized bed reduction furnace 32; Be installed in the fusing burner 313 on the melting gasifier 31, be used for accepting being ejected into melting gasifier 31 from the fine dust of dust recirculation unit 312 and with it; And circulation cyclone separator 321,331,341, be used for catching the fine dust that fluidized bed reduction furnace 32,33,34 is discharged gas, and dust is recycled to each fluid bed furnace.
Molten iron preparation facilities according to the present invention preferably includes: Venturi scrubber 35 is used to accept the first circulation cyclone separator, 341 expellant gas of first fluidized bed reduction furnace 34, to catch and to cool off remaining dust; And/or be positioned at first and second gas heaters 342 and 332 of first fluidized bed reduction furnace 34 and second fluidized bed reduction furnace, 34 upstreams, be used to accept oxygen to regulate the temperature of reducing gas.
First fluidized bed reduction furnace 34 links to each other with raw material supply pipe 34f, is used to accept fine iron ore and thin additive.
Raw material supply pipe 34f links to each other with the first fine iron ore supply pipe 34f1, and the latter links to each other with fine iron ore source (not shown) again.Pipe 34f links to each other with the second additive supply pipe 34f2, and the latter links to each other with additive source (not shown) again.
First fluidized bed reduction furnace 34 is communicated with second fluidized bed reduction furnace 33 by the first reduced iron delivery pipe 34a, to transport iron ore.Stove 34 bottoms link to each other with second fluidized bed reduction furnace 33 by the first feed tube 34b, to accept gas.Stove 34 tops link to each other with the first exhaust pipe 34c, and with discharging waste gas, and the latter links to each other with the first circulation cyclone separator 341 again.
Fluidized bed reduction furnace 34 links to each other with the first circulation cyclone separator 341 by the first dust circulation tube 34d, with the circulation dust.
Venturi scrubber 35 links to each other with the first circulation cyclone separator 341 by the second exhaust pipe 34e.
Second fluidized bed reduction furnace 33 is communicated with the 3rd fluidized bed reduction furnace 32 by the second reduced iron delivery pipe 33a.Stove 33 bottoms link to each other with the 3rd fluidized bed reduction furnace 32 by the second feed tube 33b, and its top links to each other with the 3rd waste gas delivery pipe 33c.
The 3rd waste gas delivery pipe 33c is communicated with the second circulation cyclone separator 331, and therefore, second fluidized bed reduction furnace 33 is communicated with the circulation dust with the second circulation cyclone separator 331 by the second dust circulation tube 33d.
The second circulation cyclone separator 331 links to each other with the 4th exhaust pipe 33e, and this pipe 33e links to each other with the first feed tube 34b, is used for supplying waste gas to first fluidized bed reduction furnace 34 after with gas and dust separation.Preferably, first gas heater 342 is installed between the first feed tube 34b and the 4th exhaust pipe 33e.
The 3rd fluidized bed reduction furnace 32 links to each other with the second additive supply pipe 32f, and the latter links to each other with the first additive supply pipe 34f2 again, is used for from the additive of (not shown) supply in additive source such as Wingdale or rhombspar.
The 3rd fluidized bed reduction furnace 32 links to each other with the 3rd reduced iron delivery pipe 32a, be used for the unslaked lime after final reduced iron and the calcining is delivered to melting gasifier 31, and pipe 32a links to each other with melting gasifier 31.
That is the 3rd fluidized bed reduction furnace 32 links to each other with melting gasifier 31 by the 3rd reduced iron delivery pipe 32a.
The 3rd fluidized bed reduction furnace 32 bottoms link to each other to accept gas with dust cyclone separator 311 by the 3rd feed tube 32b.The top of stove 32 links to each other with the 5th exhaust pipe 32c and is used for discharging waste gas.Pipe 32c links to each other with the 3rd circulation cyclone separator 321.
The 3rd circulation cyclone separator 321 links to each other with the 6th exhaust pipe 32e, and this pipe 32e links to each other with the second feed tube 33b, is used for giving second fluidized bed reduction furnace 33 with waste gas feed after waste gas and dust separation.Preferably, second gas heater 332 is installed between the second feed tube 33b and the 6th exhaust pipe 32e.
The 3rd fluidized bed reduction furnace 32 links to each other to accept dust with the 3rd circulation cyclone separator 321 by the 3rd dust circulation tube 32d.
Melting gasifier 31 links to each other with reducing gas delivery pipe 31a, and should link to each other with dust cyclone separator 311 by pipe 31a.Therefore, melting gasifier 31 is communicated with delivering gas with dust cyclone separator 311.
The method of utilizing molten iron preparation facilities of the present invention and reduced iron preparation facilities to prepare molten iron and reduced iron is described below.
Be described with reference to the device in Fig. 3 and 4.
Particle size is that 8mm or littler fine iron ore and additive are admitted to first fluidized bed reduction furnace 14.In first fluidized bed reduction furnace 14, the iron ore of sending into is by the reducing gas heating and the prereduction that infeed from second fluidized bed reduction furnace 13.Herein, fluidized-bed temperature should preferably remain on 700-800 ℃.This condition can prevent that iron ore is from rhombohedral iron ore (Fe
2O
3) be transformed into magnetite (Fe
3O
4).That is if temperature remains on below 650 ℃, rhombohedral iron ore stone is reduced after being transformed into magnetic iron ore.If it is also stable mutually to form magnetite, reduction rate reduces, and the time that consequently needs has just prolonged.And gas effciency is low, so fuel cost improves.If temperature remains on more than 800 ℃, first gas heater 142 requires more oxygen, and the oxygen that infeeds intensification is too fast, causes the problem of sticking together.Therefore, the most preferred temperature of fluidized-bed is about 780 ℃ or 750-800 ℃, if the gas temperature that infeeds is too low, part of oxygen enters first gas heater 142, burns partial reduction gas, thereby has regulated the temperature of fluidized-bed.The reducing gas that infeeds first fluidized bed reduction furnace 14 carried out reduction reaction in second fluid bed furnace 13, so it contains the CO of appropriate amount
2, the gas cyaniding rate is about 20%-30%.
The pre-reduced iron ore with the prereduction of 30-50% ratio is admitted to second fluidized bed reduction furnace 13 in first fluidized bed reduction furnace 14.Second fluidized bed reduction furnace 13 utilizes the reducing gas with 5-10% oxidation ratio, this reducing gas infeeds from fluidized bed calcination stove 12, so that reduction (infeeding from first fluidized bed reduction furnace 14) pre-reduced iron ore to reduction ratio is 90% or higher, thereby prepares final reduced iron.Herein, the fluidized-bed in reaction chamber preferably remains on about 850 ℃ or 830-870 ℃.If the temperature of fluidized-bed is lower than 830 ℃, reduction ratio reduces.If the temperature of fluidized-bed is higher than 870 ℃, because high temperature may stick together.
The reduced iron that is reduced in second fluidized bed reduction furnace 13 or be sent in the melting gasifier 11 and be used to form molten iron perhaps is admitted to high temperature briquetting machine 16 and is used to form the reduced iron agglomerate.
Add coal in the melting gasifier 11, produce reducing gas, be used for reducing iron ore and calcined limestone or rhombspar.Under this state, utilize heat output, the thin reduced iron of second fluidized bed reduction furnace 13 and the unslaked lime of fluidized bed calcination stove 12 melt together to produce molten iron.Different with last reduction furnace and calcining furnace, melting gasifier is a fixed-bed type, and therefore, in order to form the coal dense bed, the particle size of at least 80% coal is 8-50mm.Melting gasifier 11 can use common bituminous coal, if necessary available coke or hard coal.Yet, if the volatile organic matter that comprises in the bituminous coal is decomposed fully, at least 1000 ℃ of the temperature of melting gasifier 11 discharge gases or higher.If temperature is lower than this, organic substance (tar) incomplete decomposing then, tar (tar) is deposited on cold zone (such as water treatment device) thereby stops up flowline.If yet temperature is higher than above-mentioned nominal level, fuel cost increases, and therefore suitable temperature range is 1000-1100 ℃.The reducing gas that produces in melting gasifier 11 has above-mentioned high temperature, so it is too hot and can not directly supply with second fluidized bed reduction furnace 13.That is, if the reducing gas temperature is too high, in iron ore adhesion can appear.
In order to address this problem, fluidized-bed limestone calcination stove 12 is installed in the melting gasifier top.That is calcined limestone chemically refers to: CO
2From Wingdale CaCO
3In isolate and form CaO that is unslaked lime.This reaction needed heat, therefore, in the present invention, fluidized bed calcination stove 12 not only makes produces the required unslaked lime of molten iron, and makes the temperature of regulating reducing gas become possibility.Unslaked lime is to be used for the gangue of iron ore is separated into the additive of slag.
For example, when coal burnt in melting gasifier 11, the reducing gas amount of generation approximately was 1700-1800Nm
3/ ton molten iron is 80-120Mcal/ ton molten iron and gas is cooled to 900 ℃ of heats that discharged from 1000-1100 ℃.Simultaneously, as Wingdale (CaCO
3) when being sintered into unslaked lime (CaO), the heat that needs is the 430Kcal/Kg Wingdale.If consider that the calcining of Wingdale and the intensification of Wingdale are to be elevated to 900 ℃ from room temperature, produce the Wingdale that one ton of molten iron needs about 360Kg, therefore handling the required heat of additive is about 240Mcal/ ton molten iron.
Therefore, about 30-50% of one ton of used additive of molten iron of production can be fluidized bed calcinator 12 processing.The additive of all the other 50-70% is admitted to first fluidized bed reduction furnace 14 so that calcine reducing fine iron ore the time.Be admitted to melting gasifier 11 to produce molten iron and slag with reducing fine iron ore by fluidized bed calcination stove 12 incinerating additives.
The temperature of second fluidized bed reduction furnace 13 preferably is adjusted to about 850 ℃, and first fluidized bed reduction furnace 14 preferably is adjusted to 780 ℃.In order to regulate and to keep the constant of target temperature, second gas heater 132 and first gas heater 142 are installed in the upstream of each Reaktionsofen.The heat of the reducing gas that melting gasifier 11 produces is about 3000Kcal/Nm
3100 ℃ of required heats of the every intensification of reducing gas are about 30Kcal/Nm
3Therefore, if be used to produce reducing gas amount that one ton molten iron discharges by 17-18Nm
3The oxygen burning of (reducing gas 1%), the reducing gas of described amount can heat up 100 ℃.Herein, the required oxygen amount of molten iron per ton is 8-9Nm
3Mode according to this if regulate amount of oxygen in the injecting gas well heater, then can be elevated to temperature required temperature levels.
The method that the device that uses among Fig. 5 prepares molten iron is described below.
Particle size is that 8mm or littler fine iron ore and additive pass through the fine iron ore supply pipe 34f1 and the first additive supply pipe 34f2 charging feed supply pipe 34f respectively.Send into first fluidized bed reduction furnace 34 by raw material supply tube 34f subsequently.
Preferably produce the 50-70% of the required total additive amount of molten iron by the thin additive amount that additive supply pipe 34f2 and raw material supply tube 34f infeed.
Sent into first fluidized bed reduction furnace 34 being reduced property of fine iron ore gas (that is, from second fluidized bed reduction furnace, 33 expellant gas) preheating and prereduction, and additive is calcined, and described gas is infeeded after by second fluidized bed reduction furnace 33.
Under this state, the temperature of fluidized-bed preferably remains on 700-800 ℃.This condition can prevent that iron ore is from rhombohedral iron ore (Fe
2O
3) be transformed into magnetite (Fe
3O
4).That is if temperature remains on below 650 ℃, rhombohedral iron ore stone is reduced after being transformed into magnetic iron ore.If it is also stable mutually to form magnetite, reduction rate reduces, and the time that consequently needs has just prolonged.And gas effciency is low, so fuel cost improves.If temperature remains on more than 800 ℃, first gas heater 342 requires more oxygen, and the oxygen intensification is too fast, causes the problem of sticking together.Therefore, the most preferred temperature of fluidized-bed is different along with the kind difference of used fine iron ore, but should be about 720 ℃ or 700-750 ℃.
If it is too low to infeed the gas temperature of first fluidized bed reduction furnace 34, part of oxygen enters first gas heater 342, burns partial reduction gas, thereby has regulated the temperature of fluidized-bed.The reducing gas that infeeds first fluidized bed reduction furnace 34 carried out reduction reaction in second fluid bed furnace 33, so it contains the CO of appropriate amount
2, the gas cyaniding rate is about 30%-40%.
The pre-reduced iron ore with 30% ratio prereduction is admitted to second fluidized bed reduction furnace 33 in first fluidized bed reduction furnace 34.
Second fluidized bed reduction furnace 33 utilizes the reducing gas with 15-20% oxidation ratio, this reducing gas infeeds from the 3rd fluid bed furnace 32, so that the pre-reduced iron ore of prereduction (infeeding from first fluidized bed reduction furnace 34) for the second time to reduction ratio is 50-60%.With this understanding, the fluidized-bed temperature of second fluidized bed reduction furnace 33 preferably remains on about 780 ℃ or 780-820 ℃.
The reducing gas that has been fed to second fluidized bed reduction furnace 33 has dropped to below 800 ℃, so this temperature can be utilized.
Yet, drop to 790 ℃ or remain under 800-820 ℃ the situation at the fluidized-bed temperature of second fluidized bed reduction furnace 33, oxygen may inject second gas heater 332, with the temperature of final adjusting fluidized-bed to optimum level.
If the fluidized-bed temperature of second fluidized bed reduction furnace 33 drops to below 780 ℃, the reduction ratio that may output to the pre-reduced iron of the 3rd fluidized bed reduction furnace 32 descends, and this is not desirable.Discharge from second fluidized bed reduction furnace 33, with 50-60% prereduction rate by the iron of the prereduction second time be admitted to the 3rd fluidized bed reduction furnace 32 by the incinerating additive for the second time.
The 3rd fluidized bed reduction furnace 32 uses oxidation ratio to be 3-7%, from the reducing gas that melting gasifier 31 infeeds, so that reduce (infeeding from first fluidized bed reduction furnace 34) pre-reduced iron ore to 90% or higher reduction ratio, thereby produces final reduced iron.Herein, the fluidized-bed temperature in the 3rd fluidized bed reduction furnace 32 preferably remains on about 850 ℃ or 830-870 ℃.
If the temperature of fluidized-bed is lower than 830 ℃, reduction ratio descends.If the temperature of fluidized-bed is higher than 870 ℃, may adhesion phenomenon appear owing to high temperature.
In order to ensure the optimal temperature levels of fluidized-bed, Wingdale or rhombspar are admitted to the 3rd fluidized bed reduction furnace 32 as the temperature regulation means by the second additive supply pipe 32f.
The additive amount of sending into the 3rd fluidized bed reduction furnace 32 is to produce the required additive total amount of molten iron, less than the additive amount that infeeds first fluidized bed reduction furnace 31.
That is the additive amount of sending into the 3rd fluidized bed reduction furnace 32 is equivalent to produce the 30-50% of the required additive total amount of molten iron.Have more descriptions subsequently.
In the 3rd fluidized bed reduction furnace 32, be admitted to melting gasifier 31 with the calcining additive, so that produce molten iron by final reduction and incinerating reduced iron.
Coal is admitted to melting gasifier 31, so that melting gasifier 31 can produce reducing gas.This reducing gas is used to reduce former fine iron ore, and is used for calcining the additive such as Wingdale and rhombspar.And the combustion heat of the Chan Shenging unslaked lime that is used to melt the final fine iron ore that has reduced and finally calcined like this is so that produce molten iron.
Different with above-mentioned fluidized bed type reduction furnace, melting gasifier is a fixed-bed type, and therefore, in order to form the coal dense bed, the particle size of at least 80% coal is 8-50mm.Melting gasifier 31 can use common bituminous coal, if necessary available coke or hard coal.Yet, if the volatile organic matter that comprises in the bituminous coal is decomposed fully, at least 1000 ℃ of the temperature of melting gasifier 31 discharge gases or higher.If temperature is lower than this, organic substance (tar) incomplete decomposing then, tar (tar) is deposited on cold zone (such as water treatment device) thereby stops up flowline.If yet temperature far above above-mentioned nominal level, fuel cost increases, therefore suitable temperature range is 1000-1100 ℃.The reducing gas that produces in melting gasifier 31 has above-mentioned high temperature, so it is too hot and can not directly supply with second fluidized bed reduction furnace 32.That is, if the reducing gas temperature is too high, in iron ore adhesion can appear.
In order to solve such problem, infeed the additive such as Wingdale and rhombspar of appropriate amount to the 3rd fluidized bed reduction furnace 32.
To add Wingdale is example, and the calcined limestone chemical reaction is as follows: CO
2From Wingdale CaCO
3In isolate and form CaO that is unslaked lime.This reaction needed heat, therefore, in the present invention, fluidized bed reduction furnace 32 not only makes produces the required unslaked lime of molten iron, and makes the temperature of regulating reducing gas become possibility.Unslaked lime is to be used for the gangue of iron ore is separated into the additive of slag.
For example, when coal burnt in melting gasifier 31, the reducing gas amount of generation approximately was 1800Nm
3/ ton molten iron is 120Mcal/ ton molten iron and gas is cooled to 850 ℃ of heats that discharged from 1050 ℃.
Simultaneously, as Wingdale (CaCO
3) when being sintered into unslaked lime (CaO), the heat that needs is the 430Kcal/Kg Wingdale.If consider that the calcining of Wingdale and the intensification of Wingdale are to be elevated to 850 ℃ from room temperature, produce the Wingdale that one ton of molten iron needs about 360Kg, therefore handling the required heat of additive is about 240Mcal/ ton molten iron.Simultaneously, the pre-reduced iron temperature that will send into the 3rd fluidized bed reduction furnace of discharging from second fluidized bed reduction furnace 33 is about 780 ℃.Therefore, if be elevated to 850 ℃, the heat that needs approximately is 30Mcal.
Therefore, the additive of producing the used about 30-50% of one ton of molten iron can be fluidized bed calcinator 32 and handles.
The additive of remaining 50-70% is admitted to first fluidized bed reduction furnace 14 so that calcining simultaneously through the reduction during the second and the 3rd fluidized bed reduction furnace 33 and 32 with fine iron ore.
Be admitted to melting gasifier 31 to produce molten iron and slag with reducing fine iron ore by incinerating additive in the 3rd fluidized bed reduction furnace 32.
The additive ratio of sending between the first fluidized bed reduction furnace 34 and second fluidized bed reduction furnace 32 depends on the temperature rating and the amount of above-mentioned gas.This ratio can be regulated along with the variation of working conditions.
That is, regulate additive by this way and send into ratio: make the temperature of each fluid bed furnace control to above-mentioned optimum level.
Preferred 720 ℃ of the temperature of first fluidized bed reduction furnace 34, second fluidized bed reduction furnace 33 preferred 780 ℃, the 3rd fluidized bed reduction furnace 32 preferred 850 ℃.
Therefore, according to the performance of coal and fine iron ore, produce the required reducing gas amount of one ton of molten iron at 1500-1800Nm
3In the scope, melting gasifier 31 expellant gas temperature can change in 1000-1100 ℃ of scope.Therefore, the 30-50% that produces the required additive of one ton of molten iron is admitted to the 3rd fluidized bed reduction furnace 32 to carry out temperature regulation and calcining.Approximately the additive of 50-70% is admitted to first fluidized bed reduction furnace 34 so that calcine additive simultaneously carrying out the fine iron ore reductive through the second and the 3rd fluidized bed reduction furnace 33 and 32.
Simultaneously because thermosteresis, second and the temperature of first class pool furnace 33 and 34 drop to below the target temperature.
Therefore, in order to regulate and to keep the constant of target temperature, second gas heater 332 and first gas heater 342 to be installed in second and the upstream of first fluidized bed reduction furnace 33 and 34.
For example, high temperature (1000 ℃) to the simple control method of the suitable temp (850 ℃) of the 3rd fluidized bed reduction furnace 32 that reduces the reducing gas of melting gasifier is that a part (40%) additive is infeeded the 3rd fluidized bed reduction furnace 32, and raise second and the low temperature of first fluidized bed reduction furnace to the useful control device of optimum level be that gas heater 332 and 342 is installed.
The heat of the reducing gas that melting gasifier 31 produces is about 3000Kcal/Nm
3100 ℃ of required heats of the every intensification of reducing gas are about 30Kcal/Nm
3Therefore, if be used to produce reducing gas amount that one ton molten iron discharges by 17-18Nm
3The oxygen burning of (reducing gas 1%), the reducing gas of described amount can heat up 100 ℃.Herein, molten iron requisite oxygen amount per ton is 8-9Nm
3Mode according to this if regulate oxygen amount in the injecting gas well heater, then can be elevated to temperature required temperature levels.
According to described above the present invention, coal is used for producing reducing gas, directly uses fine iron ore.Therefore, can be simply and efficient manner prepares molten iron and reduced iron.
Claims (12)
1. a direct employing coal acts as a fuel and produces the molten iron preparation facilities of molten iron, comprising:
First fluidized bed reduction furnace (14) is used for preheating and prereduction fine iron ore;
Second fluidized bed reduction furnace (13) is used for the indirect reduction fine iron ore;
Melting gasifier (11) is used for the iron ore behind gasification of coal and the smelting reduction;
The 3rd fluidized bed calcination stove (12) is used to utilize melting gasifier (11) expellant gas calcined limestone;
Circulation cyclone separator (121,131,141) is used for catching the fine dust that first to the 3rd fluid bed furnace (12,13,14) is discharged gas, and dust is recycled to each fluid bed furnace;
Dust cyclone separator (111) is used for and will sends into dust recirculation unit (112) from the isolated dust of the reducing gas of melting gasifier 11, and will supply with the 3rd fluidized bed calcination stove (12) by isolated discharge gas from dust;
Be installed in the fusing burner (113) on the melting gasifier (11), be used for the fine dust from dust recirculation unit (112) is ejected into melting gasifier (11);
Venturi scrubber (15) is used to accept first circulation cyclone separator (141) expellant gas of first class pool furnace (14), to catch and to cool off remaining dust;
Raw material supply pipe (14f) is connected with first fluidized bed reduction furnace (14), is used to supply fine iron ore and additive; Described first fluidized bed reduction furnace (14) links to each other with described second fluidized bed reduction furnace (13) by the first reduced iron delivery pipe (14a), with the supply iron ore; Described first stove (14) links to each other with described second fluid bed furnace (13) by first feed tube (14b), with supply gas; First exhaust pipe (14c) links to each other with the top of described first stove (14), with discharging waste gas; Described pipe (14c) links to each other with the described first circulation cyclone separator (141); Described first fluidized bed reduction furnace (14) is connected to described first cyclone separator (141) to accept dust by the first dust circulation tube (14d);
Venturi scrubber (15) is connected on the described first circulation cyclone separator (141) by second exhaust pipe (14e);
Described second fluidized bed reduction furnace (13) is connected with described melting gasifier (11) by the second reduced iron delivery pipe (13a); Described second stove (13) bottom is communicated with described the 3rd fluidized bed calcination stove (12) by second feed tube (13b), to accept gas; The 3rd waste gas delivery pipe (13c) links to each other with emission gases with the top of described second stove (13); Described exhaust pipe (13c) is communicated with the described second circulation cyclone separator (131); Described second fluidized bed reduction furnace (13) is communicated with to accept dust with the described second circulation cyclone separator (131) by second circulation tube (13d);
The 4th exhaust pipe (13e) links to each other with the described second circulation cyclone separator (131) by described first feed tube (14b), is used for giving described first fluidized bed reduction furnace (14) with waste gas feed, and waste gas and dust separation are opened simultaneously;
Described the 3rd fluidized bed calcination stove (12) links to each other with Wingdale supply pipe (12f), and the latter links to each other with the Wingdale source again, so that the supply Wingdale; Described the 3rd stove (12) links to each other with unslaked lime delivery pipe (12a), is used to discharge the unslaked lime after the calcining; Described pipe (12a) links to each other with the second reduced iron delivery pipe (13a); Described the 3rd fluidized bed calcination stove (12) bottom links to each other to accept gas with described dust cyclone separator (111) by the 3rd feed tube (12b); The 5th exhaust pipe (12c) links to each other with the top of described the 3rd stove (12), with emission gases; Described the 5th exhaust pipe (12c) links to each other with described the 3rd circulation cyclone separator (121); Described calcining furnace (12) links to each other with described the 3rd circulation cyclone separator (121) by the 3rd dust circulation tube (12d), to accept dust;
Described the 3rd circulation cyclone separator (121) links to each other with the 6th exhaust pipe (12e), and the latter links to each other with feed tube (13b), described the 3rd circulation cyclone separator (121) is used for waste gas feed is arrived described second fluidized bed reduction furnace (13), and this moment, dust was separated from the gas; And
Reducing gas delivery pipe (11a) is communicated with dust cyclone separator (111), and links to each other with melting gasifier (11); The second reduced iron delivery pipe (13a) is communicated with described second fluidized bed reduction furnace 13, and links to each other with described melting gasifier (11); Described dust circulation device (112) is communicated with described dust cyclone separator (111) by a dust discharge tube (11b); Described dust circulation device (112) is communicated with fusing burner (113) on being installed in melting gasifier (11) by dust injection tube (11c).
2. molten iron preparation facilities as claimed in claim 1, it is characterized in that, first gas heater (142) and second gas heater (132) are installed in respectively between described first feed tube (14b) and described the 4th exhaust pipe (13e), and between second feed tube (13b) and the 6th exhaust pipe (12e).
3. a direct employing coal acts as a fuel and produces the reduced iron preparation facilities of reduced iron, it is characterized in that, in the described molten iron preparation facilities of claim 1, the second reduced iron delivery pipe (13a) of second fluidized bed reduction furnace (13) does not link to each other with melting gasifier (11), links to each other with the external world or links to each other to produce agglomerate with briquetting machine (16) but make.
4. reduced iron preparation facilities as claimed in claim 3, it is characterized in that, unslaked lime supply pipe (12g) is installed between fluidized bed calcination stove (12) and the described briquetting machine (16), is used for calcining back supply section unslaked lime at unslaked lime in described fluidized bed reduction furnace (12).
5. as claim 3 or 4 described reduced iron preparation facilitiess, it is characterized in that, first gas heater (142) and second gas heater (132) are installed in respectively between described first feed tube (14b) and the 4th exhaust pipe (13e), and between second feed tube (13b) and the 6th exhaust pipe (12e).
6. one kind is directly utilized coal to act as a fuel to prepare the method for molten iron, and it may further comprise the steps;
High-temperature reductibility gas is sent into fluidized-bed limestone calcination stove (12) with calcined limestone from melting gasifier (11);
Reducing gas is infeeded second fluidized bed reduction furnace (13) with the direct production reduced iron;
With the described second fluidized bed reduction furnace expellant gas infeed be positioned at second fluid bed furnace, 13 tops first fluidized bed reduction furnace (14) with preheating and prereduction fine iron ore; And the Wingdale after will calcining infeeds melting gasifier (11) to produce molten iron with final reduced iron;
It is characterized in that:
The additive Wingdale of 30-50% is fluidized bed calcinator (12) and handles, and remaining 50-70% Wingdale is handled by first fluidized bed reduction furnace (14); And
Oxygen injects first gas heater 142 and second gas heater 132, thereby with the temperature of combustion parts reducing gas by consequent thermal conditioning reducing gas.
7. method as claimed in claim 6 is characterized in that, the fluidized-bed temperature of first fluidized bed reduction furnace (14) remains on 750-800 ℃, and the fluidized-bed temperature of described second fluidized bed reduction furnace (13) remains on 830-870 ℃.
8. a direct employing coal acts as a fuel and produces the molten iron preparation facilities of molten iron, comprises;
First fluidized bed reduction furnace (34) is used for prereduction for the first time and calcining fine iron ore and thin additive;
Second fluidized bed reduction furnace (33) is used for fine iron ore of prereduction for the second time and the thin additive of calcining;
The 3rd fluidized bed reduction furnace (32), be used for being received in second fluidized bed reduction furnace (33) through reduction and incinerating fine iron ore and thin additive, and be used for additional fine iron ore and the thin additive of acceptance except that being used for first fluidized bed reduction furnace (34), and utilize the final reducing fine iron ore of melting gasifier (31) expellant gas and finally calcine thin additive;
Melting gasifier (31) is used for accepting fine iron ore and final incinerating additive from the final prereduction of described the 3rd fluidized bed reduction furnace (32), with fusing with reduce them and make molten iron;
Dust cyclone separator (311), be used for from described melting gasifier (31) send into dust recirculation unit (312) from the isolated dust of reducing gas, and will from dust, separated waste gases supply with the 3rd fluidized bed reduction furnace (32);
Be installed in the fusing burner (313) on the described melting gasifier (31), be used for the fine dust of acceptance, they are ejected into described melting gasifier (31) from described dust recirculation unit (312);
Circulation cyclone separator (321,331,341) is used for catching fine dust from described fluidized bed reduction furnace (32,33,34) expellant gas, they are looped back described each fluid bed furnace;
Venturi scrubber (35) is used to accept first circulation cyclone separator (341) expellant gas of first fluidized bed reduction furnace (34), to catch and to cool off remaining dust;
First fluidized bed reduction furnace (34) links to each other with raw material supply pipe (34f), is used to accept fine iron ore and thin additive; Described raw material supply pipe (34f) also links to each other with a fine iron ore supply pipe (34f1), and the latter links to each other with the fine iron ore source again; Described pipe (34f) links to each other with the first additive supply pipe (34f2), and the latter links to each other with the additive source again; First fluidized bed reduction furnace (34) is communicated with second fluidized bed reduction furnace (33) by the first reduced iron delivery pipe (34a), to transport iron ore; Described first stove (34) bottom links to each other with second fluidized bed reduction furnace (33) by first feed tube (34b), to accept gas; Described first stove (34) top links to each other with first exhaust pipe (34c), with discharging waste gas; First exhaust pipe (34c) links to each other with the first circulation cyclone separator (341) again; Described first fluidized bed reduction furnace (34) is communicated with the first circulation cyclone separator (341) by the first dust circulation tube (34d), with the circulation dust;
Venturi scrubber (35) links to each other with the first circulation cyclone separator (341) by second exhaust pipe (34e);
Second fluidized bed reduction furnace (33) is communicated with the 3rd fluidized bed reduction furnace (32) by the second reduced iron delivery pipe (33a); Described second stove (33) bottom links to each other with the 3rd fluidized bed reduction furnace (32) by second feed tube (33b); Described second stove (33) top links to each other with the 3rd waste gas delivery pipe (33c); The 3rd waste gas delivery pipe (33c) is communicated with the second circulation cyclone separator (331); Second fluidized bed reduction furnace (33) is communicated with the circulation dust with the second circulation cyclone separator (331) by the second dust circulation tube (33d);
The second circulation cyclone separator (331) links to each other with the 4th exhaust pipe (33e), and this pipe (33e) links to each other with first feed tube (34b), is used for gas being separated the back with fine dust to first fluidized bed reduction furnace (34) supply waste gas;
The 3rd fluidized bed reduction furnace (32) links to each other with the second additive supply pipe (32f), and the latter links to each other with the first additive supply pipe (34f1) again, is used for from the additive of additive source supply such as Wingdale or rhombspar; The 3rd fluidized bed reduction furnace (32) links to each other with the 3rd reduced iron delivery pipe (32a), the unslaked lime after being used to transport final reduced iron and calcine, and pipe (32a) links to each other with melting gasifier (31); The 3rd fluidized bed reduction furnace (32) bottom links to each other to accept gas with dust cyclone separator (311) by the 3rd feed tube (32b); The top of described the 3rd stove (32) links to each other with the 5th exhaust pipe (32c) and is used for discharging waste gas; This pipe (32c) links to each other with the 3rd circulation cyclone separator (321); The 3rd fluidized bed reduction furnace (32) links to each other with the 3rd circulation cyclone separator (321) by dust circulation tube (32d);
The 3rd circulation cyclone separator (321) links to each other with the 6th exhaust pipe (32e), and this pipe (32e) links to each other with second feed tube (33b), is used for giving second fluidized bed reduction furnace (33) with waste gas feed after waste gas and dust separation; And
Melting gasifier (31) links to each other with reducing gas delivery pipe (31a), and should link to each other with dust cyclone separator (311) by pipe (31a); Dust recirculation unit (312) is communicated with dust cyclone separator (311) by dust discharge tube (31b), and links to each other with fusing burner (313) on being installed in melting gasifier (31) by dust injection tube (31c).
9. molten iron preparation facilities as claimed in claim 8, it is characterized in that, first gas heater (342) and second gas heater (332) are installed in respectively between described first feed tube (34b) and described the 4th exhaust pipe (33e), and between second feed tube (33b) and the 6th exhaust pipe (32e).
10. one kind is directly utilized coal to act as a fuel to prepare the method for molten iron, and it may further comprise the steps:
By raw material supply tube (34f) fine iron ore and the parts of fine additive that is equivalent to the 50-70% of additive aggregate demand are sent into first fluidized bed reduction furnace (34), utilize second fluidized bed reduction furnace (33) expellant gas preheating and prereduction fine iron ore and calcining additive;
To send into second fluidized bed reduction furnace (33) from the preheating of first fluidized bed reduction furnace (34) and the additive after iron ore after the prereduction and the calcining, utilize the prereduction for the second time of the 3rd fluidized bed reduction furnace (32) expellant gas and calcining fine iron ore and additive;
With the additive of the 30-50% of required additive total amount and from described second fluidized bed reduction furnace (33) through the fine iron ore of the prereduction second time and through the second time incinerating additive send into the 3rd fluidized bed reduction furnace (32), to utilize the final prereduction of melting gasifier (31) expellant gas and calcining fine iron ore and additive; And
To send into melting gasifier (31) with fusing with reduce them from the final pre-reduced iron ore of described the 3rd fluidized bed reduction furnace (32) and final incinerating additive, thereby make molten iron.
11. method as claimed in claim 10 is characterized in that, it is further comprising the steps of: oxygen is infeeded first and second gas heaters (332) and (342) with the combustion parts reducing gas, thereby regulate the temperature of reducing gas.
12. as claim 10 or 11 described methods, it is characterized in that, the fluidized-bed temperature of first fluidized bed reduction furnace (34) remains on 700-750 ℃, the fluidized-bed temperature of described second fluidized bed reduction furnace (33) remains on 780-820 ℃, and the fluidized-bed temperature of described the 3rd fluidized bed reduction furnace (32) remains on 830-870 ℃.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| KR71434/1997 | 1997-12-20 | ||
| KR1019970071434A KR100236193B1 (en) | 1997-12-20 | 1997-12-20 | Apparatus and method for manufacturing molten pig iron and reduced iron using fluidized bed |
| KR1019980048452A KR100286689B1 (en) | 1998-11-12 | 1998-11-12 | Apparatus for manufacturing molten pig iron using fluidized bed and method for manufacturing molten pig iron using same |
| KR48452/1998 | 1998-11-12 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1248297A CN1248297A (en) | 2000-03-22 |
| CN1070926C true CN1070926C (en) | 2001-09-12 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN98802717A Expired - Lifetime CN1070926C (en) | 1997-12-20 | 1998-12-18 | Apparatus for manufacturing molten pig iron and reduced iron by utilizing fluidized bed, and method therefor |
Country Status (10)
| Country | Link |
|---|---|
| US (1) | US6277324B1 (en) |
| EP (1) | EP0973950A1 (en) |
| JP (1) | JP2000510537A (en) |
| CN (1) | CN1070926C (en) |
| AU (1) | AU722403B2 (en) |
| BR (1) | BR9807591A (en) |
| CA (1) | CA2281595A1 (en) |
| SK (1) | SK124299A3 (en) |
| TW (1) | TW400388B (en) |
| WO (1) | WO1999032668A1 (en) |
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| CN110923387B (en) * | 2019-12-12 | 2021-05-11 | 青岛理工大学 | A system and method for stepwise waste heat recovery and direct reduction of iron-containing metallurgical slag particles |
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| WO1991001799A1 (en) * | 1989-08-09 | 1991-02-21 | Cra Services Limited | Heating and treatment of particulate material |
| WO1994017214A1 (en) * | 1993-01-26 | 1994-08-04 | 'holderbank' Financière Glarus Ag | Process for producing pig iron and cement clinker |
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| DE1167368B (en) * | 1955-02-14 | 1964-04-09 | Demag Elektrometallurgie Gmbh | Operation of a low shaft furnace for refining ores |
| AT390622B (en) | 1988-10-25 | 1990-06-11 | Voest Alpine Ind Anlagen | METHOD AND INSTALLATION FOR THE PRODUCTION OF LIQUID PIG IRON |
| US5192486A (en) | 1990-03-30 | 1993-03-09 | Fior De Venezuela | Plant and process for fluidized bed reduction of ore |
| KR970003636B1 (en) * | 1994-12-31 | 1997-03-20 | 포항종합제철 주식회사 | A furnace for reduction fine coal in the manufacture of iron melts |
| AT405742B (en) * | 1996-07-10 | 1999-11-25 | Voest Alpine Ind Anlagen | METHOD FOR PRODUCING LIQUID METAL AND SYSTEM FOR IMPLEMENTING THE METHOD |
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1998
- 1998-12-18 JP JP11533608A patent/JP2000510537A/en active Pending
- 1998-12-18 US US09/367,907 patent/US6277324B1/en not_active Expired - Fee Related
- 1998-12-18 CA CA002281595A patent/CA2281595A1/en not_active Abandoned
- 1998-12-18 AU AU15115/99A patent/AU722403B2/en not_active Ceased
- 1998-12-18 BR BR9807591-8A patent/BR9807591A/en not_active Application Discontinuation
- 1998-12-18 EP EP98959286A patent/EP0973950A1/en not_active Withdrawn
- 1998-12-18 CN CN98802717A patent/CN1070926C/en not_active Expired - Lifetime
- 1998-12-18 SK SK1242-99A patent/SK124299A3/en unknown
- 1998-12-18 WO PCT/KR1998/000438 patent/WO1999032668A1/en not_active Application Discontinuation
- 1998-12-19 TW TW087121251A patent/TW400388B/en not_active IP Right Cessation
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1991001799A1 (en) * | 1989-08-09 | 1991-02-21 | Cra Services Limited | Heating and treatment of particulate material |
| WO1994017214A1 (en) * | 1993-01-26 | 1994-08-04 | 'holderbank' Financière Glarus Ag | Process for producing pig iron and cement clinker |
Also Published As
| Publication number | Publication date |
|---|---|
| BR9807591A (en) | 2000-02-22 |
| WO1999032668A1 (en) | 1999-07-01 |
| CN1248297A (en) | 2000-03-22 |
| EP0973950A1 (en) | 2000-01-26 |
| US6277324B1 (en) | 2001-08-21 |
| TW400388B (en) | 2000-08-01 |
| AU1511599A (en) | 1999-07-12 |
| JP2000510537A (en) | 2000-08-15 |
| AU722403B2 (en) | 2000-08-03 |
| CA2281595A1 (en) | 1999-07-01 |
| SK124299A3 (en) | 2000-05-16 |
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